[go: up one dir, main page]

CN112625756B - Catalytic gasification device and method for pulverized coal circulating fluidized bed - Google Patents

Catalytic gasification device and method for pulverized coal circulating fluidized bed

Info

Publication number
CN112625756B
CN112625756B CN201910905954.XA CN201910905954A CN112625756B CN 112625756 B CN112625756 B CN 112625756B CN 201910905954 A CN201910905954 A CN 201910905954A CN 112625756 B CN112625756 B CN 112625756B
Authority
CN
China
Prior art keywords
fluidized bed
gasification
gas
pyrolysis
furnace
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN201910905954.XA
Other languages
Chinese (zh)
Other versions
CN112625756A (en
Inventor
钟思青
金渭龙
徐俊
霍威
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
Original Assignee
China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by China Petroleum and Chemical Corp, Sinopec Shanghai Research Institute of Petrochemical Technology filed Critical China Petroleum and Chemical Corp
Priority to CN201910905954.XA priority Critical patent/CN112625756B/en
Publication of CN112625756A publication Critical patent/CN112625756A/en
Application granted granted Critical
Publication of CN112625756B publication Critical patent/CN112625756B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/64—Processes with decomposition of the distillation products
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/721—Multistage gasification, e.g. plural parallel or serial gasification stages
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/723—Controlling or regulating the gasification process
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/725—Redox processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0969—Carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C10J2300/0976—Water as steam
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0983—Additives
    • C10J2300/0986—Catalysts
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/12—Heating the gasifier
    • C10J2300/1223—Heating the gasifier by burners
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Industrial Gases (AREA)

Abstract

The invention discloses a pulverized coal circulating fluidized bed catalytic gasification device and a method, and discloses a pulverized coal circulating fluidized bed catalytic gasification methane increasing device, which comprises a feeder, a fluidized bed pyrolysis furnace, a fluidized bed gasification furnace, a fast bed gasification furnace, a fluidized bed combustion chamber, a fine powder sedimentation/stripping device and a fine powder sedimentation/stripping device, wherein the feeder is connected with the fluidized bed pyrolysis furnace through a feeding inclined tube, the fluidized bed gasification furnace is connected with the fluidized bed pyrolysis furnace through a pyrolysis inclined tube, the lower inlet of the fast bed gasification furnace is connected with the upper outlet of the fluidized bed gasification furnace, the upper inlet of the fast bed gasification furnace is connected with the lower outlet of the fluidized bed gasification furnace, and the fine powder sedimentation/stripping device is connected with the fluidized bed pyrolysis furnace through a gasification inclined tube. The invention also discloses a method for increasing methane yield by catalytic gasification of the pulverized coal circulating fluidized bed. The invention has the characteristics of high carbon conversion rate, high gasification intensity, high pulverized coal utilization rate, wide adaptability of gasified coal, reasonable energy utilization, stable and efficient device operation.

Description

Catalytic gasification device and method for pulverized coal circulating fluidized bed
Technical Field
The invention belongs to the field of coal gasification, and relates to a pulverized coal circulating fluidized bed catalytic gasification device and method.
Background
Coal, oil, and natural gas are three major primary energy sources in the world, wherein coal accounts for about 79% of the world's energy reserves, and coal is one of the main fuel resources for power, heat, char processing, and by-product asphalt. China is a country with coal as a main energy structure, and the coal is not changed in a long time in the future, so that the statistics shows that the coal reaches 63.7% in a primary energy consumption structure of China in 2015. Along with the increasing shortage of petroleum resources, the effective utilization of coal resources has become a strategy for sustainable development of energy sources in China. The reserve of low-rank coal in China accounts for more than 55% of the total amount of coal resources, but the low-rank coal has high moisture and low coalification degree, and has low direct combustion efficiency, so that resources are wasted, the environment is polluted, and acid rain, PM2.5, SOx, NOx and other chamber gases are discharged. The coal gasification technology is a key technology for realizing clean, efficient and comprehensive utilization of coal, is an important way for coal conversion, and is also one of key technologies for synthesizing chemicals, combined cycle power generation and coal substitute natural gas. The method is a key for realizing the sustainable development of energy in China and an effective way for solving the energy and environment problems facing the world.
The largest coal gasification technology application market in the world is in China, and at present, various coal gasification technologies successfully realize industrialized application. The method belongs to entrained flow gasification technology widely at present, and improves the carbon conversion rate at the cost of high temperature and high pressure, so that the problems of high energy consumption, difficult gas purification, severe requirements on equipment and the like are brought. Meanwhile, the excessive operation temperature of the entrained flow slag gasification technology increases the investment, maintenance and operation cost of the entrained flow. Research reports of the American electric institute (EPRI) indicate that the existing industrial entrained flow gasifier is not suitable for gasifying high ash and high ash fusion point coal, and industrial fluidized bed gasification technology is needed in the world. The fluidized bed technology has the property of adapting to high ash fusion point and high ash coal types no matter burning or gasifying, and the fact that the circulating fluidized bed boiler has successfully burned coal gangue is obvious.
Natural gas is a high-quality fuel and an important chemical raw material, and has the advantages of safety, reliability and environmental protection. With the rapid development of the economy and the acceleration of the urban step in China, the demand for natural gas is increasing. The natural gas yield of China is increasingly outstanding in the contradiction between supply and demand in order to not reach the natural gas demand, and the only dependence on import of the supply gap is compensated, so that the energy safety of China is greatly influenced. The existing technology for preparing natural gas by coal can be divided into two-step method and one-step method. The two-step coal to natural gas technology is one process of converting coal into synthetic gas (CO+H2) and methanation to obtain SNG, and includes the steps of gasifying, converting, cooling, purifying, synthesizing methane, etc. The technology for preparing natural gas by using coal as raw material through one-step method is to directly synthesize methane, and implement gasification, transformation and methanation reaction processes in gasification furnace by means of catalyst so as to obtain the synthetic gas rich in methane. The two-step coal-to-natural gas technology needs to be realized in different reactors, so that the temperature and the pressure in each reaction process are not matched, the heat loss is more when the system circulates internally, and the energy conversion efficiency of the system is reduced. The one-step coal-to-natural gas technology effectively solves the problems, realizes the coupling of logistics and heat, has higher economy and feasibility, and becomes an important research direction in the field of coal-to-natural gas.
The U.S. patent No. 4077778 proposes a process for preparing methane by a coal one-step method, which adopts alkali metal carbonate or alkali metal hydroxide as a catalyst, controls the reaction temperature in a furnace to be about 700 ℃ through superheated steam, and reacts with coal dust under the action of the catalyst to directly obtain methane-rich gas. The process needs to heat superheated steam to about 850 ℃, has higher energy consumption and lower carbon conversion rate, is difficult to maintain the reaction temperature under the condition of no external heat supply, and is still in a research and development stage.
Chinese patent CN102021037B proposes a method for preparing methane by one-step catalytic gasification of coal, wherein the gasification furnace is divided into a synthesis gas generation section, a coal methanation section and a synthesis gas methanation section, so that the combustion, gasification, methanation reaction and pyrolysis reaction are carried out in sections. However, the gasification furnace is internally provided with a plurality of layers of air distribution plates and overflow channels, the structure in the furnace is complex, the gasification efficiency and the methane yield are low, and the introduction of oxygen at the bottom of the fluidized bed easily causes ash slag to be fused and agglomerated to form massive slag, and the outlet of the gasification furnace and a gas distributor are blocked, so that the operation stability of the device is affected, and the technology does not have an industrialized device yet.
In summary, although the existing coal catalytic gasification technology solves the disadvantages of the traditional fixed bed and entrained flow gasification to a certain extent to prepare the methane-rich synthetic gas, the existing coal catalytic gasification technology is in a research and development or amplification stage and is not industrially applied yet. The adoption of fluidized bed technology and the limitation of catalytic process conditions lead to low carbon conversion and gasification intensity. Therefore, how to effectively improve the carbon conversion rate and the gasification intensity, effectively perform the heat cascade utilization of combustion, gasification and pyrolysis, reasonably couple the reaction processes of combustion, gasification, pyrolysis, transformation, methanation and the like, and realize the high-efficiency and clean utilization of the pyrolysis-gasification integrated pulverized coal quality-classifying in the true sense is the key of the development of coal gasification technology.
Disclosure of Invention
The invention aims to provide a novel pulverized coal circulating fluidized bed catalytic gasification methane increasing device and method for solving the problems of low carbon conversion rate and gasification intensity, low methane yield, low pulverized coal utilization rate and difficult utilization of low-rank coal in the prior art. The invention has the characteristics of high carbon conversion rate, high gasification intensity, high methane yield, high pulverized coal utilization rate, wide adaptability of gasified coal, reasonable energy utilization, stable and efficient device operation.
According to one aspect of the invention, there is provided a pulverized coal circulating fluidized bed catalytic gasification stimulation methane unit comprising:
A feeder;
the fluidized bed pyrolysis furnace is connected with the feeder through a feeding inclined pipe;
The fluidized bed gasification furnace is connected with the fluidized bed pyrolysis furnace through a pyrolysis inclined tube;
the lower inlet of the fast bed gasifier is connected with the upper outlet of the fluidized bed gasifier;
the upper inlet of the fluidized bed combustion chamber is connected with the lower outlet of the fluidized bed gasifier;
A fines settler/stripper connected to the fluidized bed pyrolysis furnace through a gasification chute.
According to some embodiments of the invention, the fluidized bed pyrolysis furnace comprises a dense phase zone and an olefin phase zone from bottom to top.
According to the preferred embodiment of the invention, the lower part of the side wall of the dense-phase zone is respectively provided with a pulverized coal inlet and a gasified semicoke inlet, the pulverized coal inlet is connected with a feeder through a feeding inclined tube, the gasified semicoke inlet is connected with a fine powder sedimentation/stripper through a gasified inclined tube, and the middle part of the side wall of the dense-phase zone is provided with a pyrolytic semicoke outlet which is connected with a fluidized bed gasifier through a pyrolytic inclined tube.
According to a preferred embodiment of the invention, a cyclone separator of the fluidized bed pyrolysis furnace is arranged in the olefin phase zone for separating the gas generated in the dense phase zone.
According to a preferred embodiment of the present invention, a pyrolysis fluidization gas inlet is provided in the bottom of the fluidized bed pyrolysis furnace for receiving pyrolysis fluidization gas.
According to a preferred embodiment of the invention, a pyrolysis gas outlet is provided at the top of the fluidized bed pyrolysis furnace, which is connected to the gas outlet of the cyclone separator of the fluidized bed pyrolysis furnace for discharging separated pyrolysis gas.
According to a preferred embodiment of the present invention, the fluidized-bed gasification furnace is arranged in parallel with the fluidized-bed pyrolysis furnace.
According to some embodiments of the invention, a pyrolysis semicoke inlet is arranged at the lower part of the side wall of the fluidized bed gasification furnace and is connected with the fluidized bed pyrolysis furnace through a pyrolysis chute.
According to a preferred embodiment of the present invention, a gasifying agent inlet is provided at a lower portion of a side wall of the fluidized-bed gasification furnace, the gasifying agent inlet being for receiving gasifying agent.
According to a preferred embodiment of the present invention, the lower outlet of the fluidized-bed gasification furnace is connected to the upper inlet of the fluidized-bed combustion chamber.
According to some embodiments of the invention, a gas distribution plate is arranged below the inner part of the fluidized bed combustion chamber, an ash discharge port is arranged at the bottom of the fluidized bed combustion chamber, and the ash discharge port is connected with an ash tank.
According to a preferred embodiment of the present invention, the upper outlet of the fluidized bed gasification furnace is reduced in diameter and then connected to the lower inlet of the rapid bed gasification furnace.
According to the preferred embodiment of the invention, the rapid bed gasification furnace comprises a rapid bed gasification zone, a rapid bed steam conversion zone and a rapid bed methanation zone from bottom to top, wherein a steam inlet is preferably arranged on the side wall of the rapid bed steam conversion zone, and a synthetic gas return port is preferably arranged on the side wall of the rapid bed methanation zone.
According to some embodiments of the invention, the fine powder sedimentation/stripper comprises a stripping section, a fine powder sedimentation section and a fine powder sedimentation/stripper cyclone separator, wherein a stripping gas inlet is arranged at the lower part of the side wall of the fine powder sedimentation/stripper and is used for receiving stripping gas, a semicoke outlet is arranged at the lower part of the side wall of the fine powder sedimentation/stripper and is connected with a fluidized bed pyrolysis furnace through a gasification inclined pipe, and a synthesis gas outlet is arranged at the top of the fine powder sedimentation/stripper and is connected with a gas outlet of the fine powder sedimentation/stripper cyclone separator and is used for discharging separated synthesis gas.
According to a preferred embodiment of the present invention, a rapid bed cyclone is provided inside the fine powder settling/stripper, which is connected to an upper outlet of the rapid bed gasifier.
According to some embodiments of the invention, the apparatus further comprises an aftertreatment system comprising:
a first gas-solid fast separator connected to a pyrolysis gas outlet of the fluidized bed pyrolysis furnace;
The gas-liquid separation device is connected with the first gas-solid rapid separator;
A second gas-solids fast separator connected to the synthesis gas outlet of the fines settling/stripper;
and the gas separation device is connected with the second gas-solid rapid separator and the gas-liquid separation device.
According to a preferred embodiment of the invention, the first gas-solid fast separator is provided with a pyrolysis gas inlet, a first gas-solid fast separator gas outlet and a fly ash outlet, the pyrolysis gas inlet being connected to the pyrolysis gas outlet of the fluidized bed pyrolysis furnace, the gas outlet being connected to a gas-liquid separation device.
According to a preferred embodiment of the invention, the gas-liquid separation device is provided with a gas inlet of the gas-liquid separation device, a tar outlet and a gas outlet of the gas-liquid separation device, the gas inlet of the gas-liquid separation device being connected to the gas outlet of the first gas-solid fast separator, the gas outlet of the gas-liquid separation device being connected to the gas separation device.
According to a preferred embodiment of the invention, the second gas-solid flash separator is provided with a synthesis gas inlet connected to the synthesis gas outlet of the fines sedimentation/stripping vessel, a fly ash outlet and a second gas-solid flash separator gas outlet connected to a gas separation device.
According to a preferred embodiment of the invention, the gas separation device is provided with a gas inlet, a recycle gas outlet and a synthesis gas outlet, the gas inlet being connected to the gas outlet of the gas-liquid separation device and to the gas outlet of the second gas-solid fast separator, respectively, the recycle gas outlet being connected to the synthesis gas return of the fast bed methanation region.
According to some embodiments of the invention, the device further comprises a catalyst system comprising a catalyst recovery device and a catalyst loading device, wherein the upstream of the catalyst recovery device is connected with the ash tank, the downstream of the catalyst recovery device is connected with the catalyst loading device, and the upstream of the catalyst loading device is connected with the catalyst recovery device, and the downstream of the catalyst loading device is connected with the feeder.
According to a preferred embodiment of the invention, the catalyst recovery device is provided with an inlet connected to the ash tank, an ash outlet connected to the catalyst loading device, and a catalyst outlet.
According to a preferred embodiment of the present invention, the catalyst loading device is provided with a first catalyst inlet for replenishing the catalyst, a second catalyst inlet for adding the carrier, a carrier inlet for connecting with the feeder, and a catalyst outlet.
According to a preferred embodiment of the invention, a pyrolysis semicoke return valve is arranged on the pyrolysis chute, which is a non-mechanical return valve, preferably a U valve, a J valve, an L valve or an M valve. And introducing loosening gas into the pyrolysis semicoke valve, and controlling the circulation amount of the pyrolysis semicoke by adjusting the air quantity of the loosening gas, or the bed density of the fluidized bed gasification furnace, or the material level of the fluidized bed pyrolysis furnace.
According to a preferred embodiment of the invention, a gasification carbocoal return valve is arranged on the gasification inclined tube, which is a non-mechanical return valve, preferably a U valve, a J valve, an L valve or an M valve. And introducing loosening gas into the gasification semicoke returning valve, and controlling the circulation quantity of gasification semicoke, or the material level of the fine powder sedimentation/stripper or the temperature of the fluidized bed pyrolysis furnace by adjusting the air quantity of the loosening gas.
According to another aspect of the invention, there is provided a method for increasing methane production by catalytic gasification of pulverized coal circulating fluidized bed, which adopts the device, and comprises the following steps:
(a) The pulverized coal raw material is sent into a fluidized bed pyrolysis furnace by a feeder, and is mixed with high-temperature gasified semicoke in the fluidized bed pyrolysis furnace to be heated, and the pulverized coal undergoes pyrolysis reaction to generate pyrolysis semicoke and pyrolysis gas;
(b) The pyrolysis semicoke enters a fluidized bed gasifier through a pyrolysis inclined tube, contacts with gasifying agents, and performs gasification reaction in the fluidized bed gasifier and a fast bed gasifier to generate synthesis gas and carbon-containing gasification semicoke;
(c) The synthesis gas enters a fine powder sedimentation/stripping device to separate high-temperature gasification semicoke, and the high-temperature gasification semicoke enters a fluidized bed pyrolysis furnace through a gasification inclined tube;
(d) The carbon-containing gasified semicoke downwards enters a fluidized bed combustion chamber from a fluidized bed gasifier to undergo a combustion reaction to produce ash slag and high-temperature gas, and the high-temperature gas upwards enters the fluidized bed gasifier to be used as a gasifying agent.
According to some embodiments of the invention, the pulverized coal feedstock comprises pulverized coal and at least one of a catalyst and biomass, preferably the catalyst comprises at least one of an alkali metal, an alkaline earth metal, and a transition metal.
According to the preferred embodiment of the invention, the catalyst is loaded on the pulverized coal in a manner of an impregnation method, a dry mixing method or an ion exchange method, and the loading of the catalyst accounts for 0.1-30% of the mass of the pulverized coal.
According to some embodiments of the invention, the pulverized coal raw material is fed into a dense-phase region of the fluidized bed pyrolysis furnace by a feeder, is mixed with high-temperature gasified semicoke in the dense-phase region and heated, the pulverized coal undergoes pyrolysis reaction to generate pyrolysis semicoke and pyrolysis gas, the pyrolysis semicoke enters the fluidized bed gasification furnace through a pyrolysis inclined tube, the pyrolysis gas carries fine pulverized coal, upwards enters an olefin-phase region and carries out gas-solid separation through a cyclone separator of the fluidized bed pyrolysis furnace, solids (fine coal powder) return to the dense-phase region, gas leaves the fluidized bed pyrolysis furnace and sequentially enters a first gas-solid rapid separator and a gas-liquid separation device, fly ash is separated in the first gas-solid rapid separator, tar is separated by the gas-liquid separation device, and then the tar enters the gas separation device.
According to a preferred embodiment of the invention, the pyrolysis pressure of the fluidized bed pyrolysis furnace is 0-6.5MPa, the pyrolysis temperature is 400-800 ℃, and/or the average density of pulverized coal in a dense phase zone of the fluidized bed pyrolysis furnace is 200-550kg/m 3, and the superficial linear velocity is 0.1-1.0m/s.
According to a preferred embodiment of the present invention, the pyrolysis fluidization gas is introduced into the fluidized bed pyrolysis furnace through a pyrolysis fluidization gas inlet at the bottom of the fluidized bed pyrolysis furnace, wherein the pyrolysis fluidization gas comprises at least one of steam, CO 2, CO, hydrogen, and inert gas.
According to some embodiments of the invention, the pyrolysis semicoke enters the lower part of the fluidized bed gasifier through the pyrolysis inclined tube, contacts with gasifying agent, and performs gasification reaction in the fluidized bed gasifier and the fast bed gasifier to generate synthesis gas and carbon-containing gasification semicoke. And introducing steam into the fast bed steam conversion zone while the fast bed gasifier is in gasification reaction, performing steam reaction (CO+H 2O＝CO2+H2) to adjust the H 2/CO ratio, introducing circulating synthetic gas into the fast bed methanation zone, and performing methanation reaction (CO+3H 2＝CH4+H2 O) to improve the yield of methane in the product.
According to the preferred embodiment of the invention, the loosening gas is introduced into the pyrolysis semicoke valve, and the circulation amount of the pyrolysis semicoke, the bed density of the fluidized bed gasification furnace or the material level of the fluidized bed pyrolysis furnace is controlled by adjusting the air quantity of the loosening gas.
According to a preferred embodiment of the invention, the loosening gas comprises at least one of water vapor, CO 2, CO, air, oxygen, and an inert gas.
According to a preferred embodiment of the invention, the gasifying agent is a high-temperature gas from a fluidized bed combustion chamber or a gasifying agent from outside introduced through a gasifying agent inlet, and the gasifying agent comprises water vapor and/or CO 2.
According to a preferred embodiment of the invention, the gasification pressure of the fluidized bed gasifier is 0-6.5MPa, the gasification temperature is 700-1200 ℃, the average density of pulverized coal is 200-450kg/m 3, and the average superficial linear velocity is 0.2-1.2m/s.
According to the preferred embodiment of the invention, the gasification pressure of the rapid bed steam conversion zone is 0-6.5MPa, the gasification temperature is 700-1000 ℃, and/or the gasification pressure of the rapid bed methanation zone is 0-6.5MPa, the gasification temperature is 700-900 ℃, and/or the average density of pulverized coal in the rapid bed gasifier is 50-150 kg/m 3, and the average air tower linear speed is 1.0-3.0 m/s.
According to some embodiments of the invention, the synthesis gas exiting the rapid bed gasifier is entrained with unvaporized semicoke fines, which first enter the rapid bed cyclone for primary gas-solid separation, the solids fall into the stripping section of the fines settler/stripper, and the gas enters the settling section of the fines settler/stripper.
According to a preferred embodiment of the invention, the gas coming out of the fast bed cyclone is fed into the settling section of the fines settling/stripper and the fines settling/stripper cyclone for further separation of solids, which solids fall into the stripping section of the fines settling/stripper, and the gas leaves the fines settling/stripper to a second gas-solids fast separator for separation of fly ash and is fed into the gas separation device together with the gas coming out of the gas-liquid separation device, which separates methane from the synthesis gas into recycle gas (methane-lean gas) and methane-rich synthesis gas, and part of the gas coming out of the gas separation device is recycled back to the fast bed methanation zone and the other part is discharged as methane-rich synthesis gas.
According to the preferred embodiment of the invention, the stripping gas is introduced into the stripping section of the fine powder sedimentation/stripping device through the stripping gas inlet, the solid in the stripping section is stripped, fly ash carried in the solid is removed, and the high-temperature gasified semicoke is obtained, and enters the fluidized bed pyrolysis furnace through the gasification inclined tube.
According to a preferred embodiment of the present invention, the stripping gas comprises at least one of steam, CO 2, CO and inert gas.
According to the preferred embodiment of the invention, the gasification semicoke returning valve is filled with the loose air, and the circulation quantity of gasification semicoke, the material level of the fine powder sedimentation/stripper or the temperature of the fluidized bed pyrolysis furnace is controlled by adjusting the air quantity of the loose air.
According to a preferred embodiment of the invention, the loosening gas comprises at least one of water vapor, CO2, CO, air, oxygen and an inert gas.
According to a preferred embodiment of the present invention, the pressure of the fine powder settling/stripper is 0-6.5MPa, the temperature is 700-1200 ℃, the average density of pulverized coal is 350-550kg/m 3, and the average superficial linear velocity is 0.1-0.5m/s.
According to some embodiments of the invention, the carbonaceous gasification semicoke enters a fluidized bed combustion chamber downwards from a fluidized bed gasification furnace, contacts with an oxidant to generate combustion reaction to produce ash slag and high-temperature gas, the high-temperature gas enters the fluidized bed gasification furnace upwards to serve as the gasification agent and provide heat for gasification reaction, the ash slag is discharged to an ash slag tank through an ash slag discharge port and then enters a catalyst recovery device, catalyst and ash slag are separated, the ash slag is discharged outwards, the recovered catalyst enters a catalyst loading device, and the catalyst is loaded on a carrier and then is conveyed to a feeder as raw materials.
According to a preferred embodiment of the invention, the oxidizing agent comprises air and/or oxygen.
According to a preferred embodiment of the invention, the carrier comprises pulverized coal, char and other carbonaceous material.
According to a preferred embodiment of the invention, the catalyst and/or biomass may also be replenished therein through the second catalyst inlet of the catalyst loading means.
According to a preferred embodiment of the invention, the combustion pressure of the fluidized bed combustion chamber is 0-6.5MPa, the combustion temperature is 800-1500 ℃, the average density of pulverized coal is 300-450kg/m 3, and the average superficial linear velocity is 0.2-0.6m/s.
According to the technical scheme, the pulverized coal raw material is pyrolyzed in the pyrolysis furnace to obtain pyrolysis gas (comprising coal tar) and gasification raw material-pyrolysis semicoke, and the gasification raw material is obtained through pyrolysis, so that the application range of coal types is enlarged. And (3) carrying out gasification reaction of pyrolysis semicoke particles in a gasification furnace to generate synthesis gas. Most of unvaporized high-temperature gasified semicoke particles are used as a heat carrier and circularly enter a pyrolysis furnace to be used as a heat source for pyrolysis, so that the energy consumption is reduced, and the cost of the heat carrier added in the traditional process is saved. And a small part of gasified semicoke particles which are not gasified enter a combustion chamber to perform combustion reaction with oxygen, so that semicoke is converted into ash, and the carbon conversion rate and the utilization rate of carbon residue are improved. The heat generated by the combustion reaction is used to provide heat consumption and heat loss in the gasification reaction and to provide the necessary gasifying agent for the gasification reaction. The invention is specially provided with a fine powder sedimentation/stripping device, and aims to remove fly ash carried in high-temperature gasified semicoke entering a pyrolysis furnace, thereby reducing the fly ash carried in pyrolysis gas, avoiding the blockage of the fly ash to related equipment and reducing the difficulty of liquid-solid separation.
According to the invention, the pyrolysis, gasification, combustion, gasification, shift, methanation and other processes are coupled, the partition coupling of gasification, shift and methanation is realized in one gasification furnace, the methane yield of one-way reaction is effectively improved, the separated synthesis gas is circulated and returned to the methanation region of the gasification furnace for further methanation reaction, the methane-rich synthesis gas can be produced, the byproduct coal tar is produced, and the quality and grading utilization of low-rank coal is realized. The catalyst can be recycled after separation and recovery, so that the high-efficiency, clean and reasonable comprehensive utilization of coal is realized.
Compared with the prior art, the gasification outlet carbon conversion rate in the reactor is increased to 98%, the methane content in the synthesis gas is increased to 15%, and the yield of tar is increased by 10%.
Drawings
FIG. 1 is a schematic diagram of a pulverized coal circulating fluidized bed catalytic gasification methane-increasing device of the invention:
In FIG. 1, the device 1 is a feeder, the device 2 is a fluidized bed pyrolysis furnace, the device 3 is a dense-phase region of the fluidized bed pyrolysis furnace, the device 4 is a dilute-phase region of the fluidized bed pyrolysis furnace, the device 5 is a cyclone separator of the fluidized bed pyrolysis furnace, the device 6 is a pyrolysis semicoke material returning valve, the device 7 is a fluidized bed combustion chamber, the device 8 is a fluidized bed gasification furnace, the device 9 is a rapid bed gasification furnace, the device 10 is a rapid bed gasification region, the device 11 is a rapid bed water vapor conversion region, the device 12 is a rapid bed methanation region, the device 13 is a fine powder sedimentation/stripper, the device 14 is a cyclone separator of the rapid bed gasification furnace, the device 15 is a stripping section, the device 16 is a fine powder sedimentation section, the device 17 is a fine powder sedimentation/stripper cyclone separator, the device 18 is a gas distribution plate, the device 19 is an ash residue outlet, the device 20 is an ash residue tank, the device 21 is a gasification semicoke material returning valve, the device 22 is a material feeding inclined tube, the device 23 is a pyrolysis inclined tube, the device 24 is a gasification inclined tube, the device 25 is a first gas-solid rapid separator, the device 26 is a gas-liquid separator, the device 27 is a second gas-solid rapid separator, the device 28 is a gas separator, the device 29 is a catalyst device, the device 30 is a catalyst carrier, the device is 30 is a fine powder carrier, the device 17 is a fine powder carrier, the fine coal is F, the catalyst and the catalyst is F, the catalyst and the coal is F or the carrier and the coal is F or the coal is F.
Detailed Description
The present invention is further illustrated by, but not limited to, the following examples.
In the following examples, the evaluation and test methods involved are as follows:
the carbon conversion rate is calculated based on carbon residue in ash, and the specific formula is as follows:
Cc= (1-C ash/Craw) ×100%, where CC is carbon conversion, C ash is carbon content in ash, C raw is carbon content in pulverized coal feedstock;
measuring the gas component by an on-line gas chromatograph external standard method to measure the methane content in the synthesis gas;
The tar yield is calculated through the mass balance of gas, liquid and solid products, and the specific formula is as follows:
Y tar＝(Mraw-Mgas-Mash)/Mraw x 100%, where Y tar is tar yield, M raw is pulverized coal feed mass flow, M gas is product gas mass flow, and M ash is ash mass flow.
[ Example 1 ]
The method comprises the steps of feeding raw materials into a dense-phase area (3) of a fluidized bed pyrolysis furnace (2) by a feeder (1), mixing the raw materials with high-temperature gasified semicoke/ash residues from a gasification furnace, heating the mixture to carry out pyrolysis reaction, enabling pyrolysis gas with fine coal powder to enter a subsequent first gas-solid rapid separator (25) to remove fly ash K after gas-solid separation, enabling the gas-solid rapid separator to separate tar L products by a gas-liquid separation device (26), enabling the fine coal powder to enter a gas separation device (28), enabling the fine coal powder to return to the dense-phase area (3), enabling the pyrolysis semicoke to enter a fluidized bed gasification furnace (8) to contact with a gasifying agent D after controlling circulation amount, and enabling gasification reaction to take place in the fluidized bed gasification furnace (8) and the rapid bed gasification furnace (9) to generate synthetic gas. And (3) introducing steam E into the rapid bed steam conversion area (11) while the rapid bed gasifier (9) carries out gasification reaction, carrying out steam conversion reaction to adjust the H 2/CO ratio, and introducing circulating synthetic gas into the rapid bed methanation area (12) to carry out methanation reaction to improve the yield of methane in the product. After being separated, the synthesis gas with the carbocoal fine powder enters a settling section (16) at the upper part of the fine powder settling/stripping device (13), and the gasification carbocoal which is not gasified falls into a stripping section (15) at the lower part of the fine powder settling/stripping device (13). After the synthetic gas coming out from the top of the cyclone separator (14) of the rapid bed gasification furnace enters a subsequent second gas-solid rapid separator (27) to remove the fly ash K, the synthetic gas is mixed with the gas from the gas-liquid separation device (26) and enters the gas separation device (28), wherein part of the synthetic gas is recycled to the rapid bed methanation region (12) as circulating gas, and methanation reaction further occurs, so that the methane yield is improved. The stripping section (15) adopts stripping gas F to strip unreacted carbon-containing semicoke, reduces fly ash carried in the unreacted carbon-containing semicoke, the stripped carbon-containing semicoke and ash compounds enter the lower part of a dense phase zone (3) of the fluidized bed pyrolysis furnace (2) after the circulation quantity is controlled, are mixed with fresh pulverized coal raw materials, heat the fresh pulverized coal raw materials for pyrolysis, the carbon-containing gasified semicoke and ash fall into a fluidized bed combustion chamber (7) from the bottom of the fluidized bed gasification furnace (8), contact and mix with an oxidant C, and undergo combustion reaction to convert the carbon-containing semicoke into ash, and are discharged out of the device periodically or continuously. The high-temperature gas generated by combustion enters the fluidized bed gasifier (8) upwards to serve as a gasifying agent and provides heat for a gasifying medium, the catalyst-containing ash discharged from the ash tank (20) is subjected to heat exchange and then enters the catalyst recovery device (29) to recover the catalyst, and then is discharged, and the recovered catalyst enters the catalyst loading device (30) to be recycled.
Lignite is adopted as a raw material in the reaction flow. The pyrolysis pressure of the fluidized bed pyrolysis furnace (2) is 0, the pyrolysis temperature is 400 ℃, the average density of pulverized coal in a dense-phase zone (3) of a reactor of the fluidized bed pyrolysis furnace (2) is 200 kg/m 3, and the line speed of a hollow tower in the dense-phase zone (3) of the reactor of the fluidized bed pyrolysis furnace (2) is 1.0 m/s; the gasification pressure 0 and the gasification temperature 700 ℃ of the fluidized bed gasification furnace (8), the average density of pulverized coal in the fluidized bed gasification furnace (8) is 200 kg/m 3, the average air tower linear velocity in the fluidized bed gasification furnace (8) is 1.2 m/s, the gasification pressure 0 and the gasification temperature 700 ℃ of the rapid bed gasification zone (10), the gasification pressure 0 and the gasification temperature 700 ℃ of the rapid bed steam conversion zone (11), the gasification pressure 0 and the gasification temperature 700 ℃ of the rapid bed methanation zone (12), the average density of pulverized coal in the rapid bed gasification furnace (9) is 50 kg/m 3, the average air tower linear velocity is 3.0 m/s, the combustion pressure 0 and the combustion temperature 800 ℃ of the fluidized bed combustion chamber (7) are 300 kg/m 3, the average air tower linear velocity in the fluidized bed combustion chamber (7) is 0.6 m/s, the pressure 0 and the temperature 700 ℃ of the fine powder sedimentation/stripper (9) are 350 kg/m 3, and the average air tower linear velocity in the fine powder sedimentation/stripper (9) is 0.5 m/s. Wherein the pyrolysis fluidization gas B adopts inert atmosphere, and the gasifying agent D adopts water vapor. Through the scheme, the conversion rate of the gasification outlet carbon in the reactor is 93%, the methane content in the synthesis gas is improved to 12.8%, and the tar yield is 8.1%. The detailed results are shown in Table 1.
[ Example 2 ]
The reaction scheme was the same as in example 1. Lignite is adopted as a raw material in the reaction flow. The pyrolysis pressure of the fluidized bed pyrolysis furnace (2) is 6.5MPa, the pyrolysis temperature is 400 ℃, the average density of pulverized coal in a dense-phase zone (3) of a reactor of the fluidized bed pyrolysis furnace (2) is 200 kg/m 3, the linear velocity of a hollow tower in the dense-phase zone (3) of the reactor of the fluidized bed pyrolysis furnace (2) is 1.0 m/s, the gasification pressure of the fluidized bed gasification furnace (8) is 0, the gasification temperature is 700 ℃, the average linear velocity of pulverized coal in the fluidized bed gasification furnace (8) is 1.2 m/s, the gasification pressure of a fast bed gasification zone (10) is 0, the gasification temperature is 700 ℃, the gasification pressure of a fast bed steam conversion zone (11) is 0, the gasification temperature is 700 ℃, the average density of pulverized coal in a fast bed gasification zone (12) is 50 kg/m 3, the average linear velocity of a hollow tower is 3.0 m/s, the combustion pressure of a fluidized bed combustion chamber (7) is 200 kg/m 3, the combustion temperature is 800 ℃, the average linear velocity of the fluidized bed combustion chamber is 300 kg/m/s, and the average density of fine powder in a fluidized bed combustion chamber is 34.0 kg/m/s, and the average density of fine powder in a fluidized bed combustion chamber is 0 m/s (3.0 m/s). Wherein the pyrolysis fluidization gas B adopts inert atmosphere, and the gasifying agent D adopts water vapor. By the scheme, the conversion rate of the gasification outlet carbon in the reactor is 93%, the methane content in the synthesis gas is improved to 13.2%, and the tar yield is 7.7%. The detailed results are shown in Table 1.
[ Example 3]
The reaction scheme was the same as in example 1. Lignite is adopted as a raw material in the reaction flow. The pyrolysis pressure of the fluidized bed pyrolysis furnace (2) is 0, the pyrolysis temperature is 800 ℃, the average density of pulverized coal in a dense-phase zone (3) of a reactor of the fluidized bed pyrolysis furnace (2) is 200 kg/m 3, and the line speed of a hollow tower in the dense-phase zone (3) of the reactor of the fluidized bed pyrolysis furnace (2) is 1.0 m/s; the gasification pressure 0 and the gasification temperature 1200 ℃ of the fluidized bed gasification furnace (8), the average density of pulverized coal in the fluidized bed gasification furnace (8) is 200 kg/m 3, the average air tower linear velocity in the fluidized bed gasification furnace (8) is 1.2 m/s, the gasification pressure 0 and the gasification temperature 1200 ℃ of the rapid bed gasification zone (10), the gasification pressure 0 and the gasification temperature 1000 ℃ of the rapid bed steam conversion zone (11), the gasification pressure 0 and the gasification temperature 900 ℃ of the rapid bed methanation zone (12), the average density of pulverized coal in the rapid bed gasification furnace (9) is 50 kg/m 3, the average air tower linear velocity is 3.0 m/s, the combustion pressure 0 and the combustion temperature 1500 ℃ of the fluidized bed combustion chamber (7), the average air tower linear velocity in the fluidized bed combustion chamber (7) is 0.6 m/s, the pressure 0 and the temperature 1200 ℃ of the fine powder sedimentation/stripper (9), the average density of pulverized coal is 350 kg/m 3, and the average air tower linear velocity in the fine powder sedimentation/stripper (9) is 0.5 m/s. Wherein the pyrolysis fluidization gas B adopts inert atmosphere, and the gasifying agent D adopts water vapor. By the scheme, the gasification outlet carbon conversion rate in the reactor is 96%, the methane content in the synthesis gas is improved to 16.3%, and the tar yield is 5.6%. The detailed results are shown in Table 1.
[ Example 4]
The reaction scheme was the same as in example 1. Lignite is adopted as a raw material in the reaction flow. The pyrolysis pressure of the fluidized bed pyrolysis furnace (2) is 0, the pyrolysis temperature is 800 ℃, the average density of pulverized coal in a dense-phase zone (3) of a reactor of the fluidized bed pyrolysis furnace (2) is 200 kg/m 3, the linear velocity of a hollow tower in the dense-phase zone (3) of the reactor of the fluidized bed pyrolysis furnace (2) is 1.0 m/s, the gasification pressure of the fluidized bed gasification furnace (8) is 6.5MPa, the gasification temperature is 1200 ℃, the average linear velocity of the pulverized coal in the fluidized bed gasification furnace (8) is 1.2 m/s, the gasification pressure of a fast bed gasification zone (10) is 6.5MPa, the gasification temperature is 1200 ℃, the gasification pressure of a fast bed steam conversion zone (11) is 6.5MPa, the gasification temperature is 1000 ℃, the average density of the fast bed gasification zone (12) is 6.5MPa, the gasification temperature is 900 ℃, the average density of the fast bed gasification furnace (9) is 50 kg/m 3, the average linear velocity of the average hollow tower is 3.0 m/s, the average combustion pressure of the fluidized bed combustion chamber (7.5 MPa, the average hollow tower linear velocity of the average density of the fluidized bed gasification chamber (8) is 1.2 m/s, the average density of the fluidized bed combustion chamber (7.5 MPa, the average density of the fluidized bed combustion chamber is 300 m/s, the average density of the fluidized bed combustion chamber is 0.34 m/s, the average density of the pulverized coal in the fluidized bed combustion chamber is 300 m/s, and the average density of the fluidized bed combustion chamber is 300 m/s, and the average density of the pulverized coal is 0 m/s. Wherein the pyrolysis fluidization gas B adopts inert atmosphere, and the gasifying agent D adopts water vapor. By the scheme, the gasification outlet carbon conversion rate in the reactor is 96%, the methane content in the synthesis gas is improved to 17.6%, and the tar yield is 5.2%. The detailed results are shown in Table 1.
[ Example 5]
The reaction scheme was the same as in example 1. Lignite is adopted as a raw material in the reaction flow. The pyrolysis pressure of the fluidized bed pyrolysis furnace (2) is 0, the pyrolysis temperature is 800 ℃, the average density of pulverized coal in a dense-phase zone (3) of a reactor of the fluidized bed pyrolysis furnace (2) is 550 kg/m 3, the linear velocity of a hollow tower in the dense-phase zone (3) of the reactor of the fluidized bed pyrolysis furnace (2) is 0.1 m/s, the gasification pressure of a fluidized bed gasification furnace (8) is 6.5MPa, the gasification temperature is 1200 ℃, the average linear velocity of the pulverized coal is 450 kg/m 3, the average linear velocity of the hollow tower in the fluidized bed gasification furnace (8) is 0.2 m/s, the gasification pressure of a fast bed gasification zone (10) is 6.5MPa, the gasification temperature is 1200 ℃, the gasification pressure of a fast bed steam conversion zone (11) is 6.5MPa, the gasification temperature is 1000 ℃, the gasification pressure of a fast bed methanation zone (12) is 6.5MPa, the gasification temperature is 900 ℃, the average density of the fluidized bed gasification furnace (9) is 150 kg/m 3, the average linear velocity of the average hollow tower is 1.0 m/s, the average combustion pressure of the fluidized bed combustion chamber (7) is 6.5MPa, the average hollow tower linear velocity of the average density of the fluidized bed combustion chamber is 0.2 m/s, the average density of the fluidized bed combustion chamber is 500 kg/s, the average density of the pulverized coal is 0.34 m/s, and the average density of the fluidized bed combustion chamber is 500 kg of the pulverized coal is 0.2 m/s. Wherein the pyrolysis fluidization gas B adopts inert atmosphere, and the gasifying agent D adopts water vapor. By the scheme, the gasification outlet carbon conversion rate in the reactor is 96%, the methane content in the synthesis gas is improved to 18.0%, and the tar yield is 5.1%. The detailed results are shown in Table 1.
[ Example 6]
The reaction scheme was the same as in example 1. Lignite is adopted as a raw material in the reaction flow. The pyrolysis pressure of the fluidized bed pyrolysis furnace (2) is 0, the pyrolysis temperature is 600 ℃, the average density of pulverized coal in a dense-phase zone (3) of a reactor of the fluidized bed pyrolysis furnace (2) is 550 kg/m 3, and the line speed of a hollow tower in the dense-phase zone (3) of the reactor of the fluidized bed pyrolysis furnace (2) is 0.1 m/s; the gasification pressure of the fluidized bed gasification furnace (8) is 6.5MPa, the gasification temperature is 900 ℃, the average density of pulverized coal is 450 kg/m 3, the average empty tower linear speed in the fluidized bed gasification furnace (8) is 0.2 m/s, the gasification pressure of the rapid bed gasification zone (10) is 6.5MPa, the gasification temperature is 900 ℃, the gasification pressure of the rapid bed steam conversion zone (11) is 6.5MPa, the gasification temperature is 850 ℃, the gasification pressure of the rapid bed methanation zone (12) is 6.5MPa, the gasification temperature is 800 ℃, the average density of pulverized coal in the rapid bed gasification furnace (9) is 150 kg/m 3, the average empty tower linear speed is 1.0 m/s, the combustion pressure of the fluidized bed combustion chamber (7) is 6.5MPa, the combustion temperature is 1100 ℃, the average density is 500 kg/m 3, the average empty tower linear speed in the fluidized bed combustion chamber (7) is 0.2 m/s, the pressure of the fine powder sedimentation/stripper (9) is 6.5MPa, the temperature is 850 m/s, and the average empty tower density in the pulverized coal sedimentation device (34.34 kg/m/s). Wherein the pyrolysis fluidization gas B adopts inert atmosphere, and the gasifying agent D adopts water vapor. By the scheme, the conversion rate of carbon at the gasification outlet in the reactor is 95%, the methane content in the synthesis gas is improved to 18.5%, and the tar yield is 9.9%. The detailed results are shown in Table 1.
[ Example 7]
The reaction scheme was the same as in example 1. The raw materials in the reaction flow adopt lignite+5% K 2CO3. The pyrolysis pressure of the fluidized bed pyrolysis furnace (2) is 0, the pyrolysis temperature is 600 ℃, the average density of pulverized coal in a dense-phase zone (3) of a reactor of the fluidized bed pyrolysis furnace (2) is 550 kg/m 3, and the line speed of a hollow tower in the dense-phase zone (3) of the reactor of the fluidized bed pyrolysis furnace (2) is 0.1 m/s; the gasification pressure of the fluidized bed gasification furnace (8) is 6.5MPa, the gasification temperature is 900 ℃, the average density of pulverized coal is 450 kg/m 3, the average empty tower linear speed in the fluidized bed gasification furnace (8) is 0.2 m/s, the gasification pressure of the rapid bed gasification zone (10) is 6.5MPa, the gasification temperature is 900 ℃, the gasification pressure of the rapid bed steam conversion zone (11) is 6.5MPa, the gasification temperature is 850 ℃, the gasification pressure of the rapid bed methanation zone (12) is 6.5MPa, the gasification temperature is 800 ℃, the average density of pulverized coal in the rapid bed gasification furnace (9) is 150 kg/m 3, the average empty tower linear speed is 1.0 m/s, the combustion pressure of the fluidized bed combustion chamber (7) is 6.5MPa, the combustion temperature is 1100 ℃, the average density is 500 kg/m 3, the average empty tower linear speed in the fluidized bed combustion chamber (7) is 0.2 m/s, the pressure of the fine powder sedimentation/stripper (9) is 6.5MPa, the temperature is 850 m/s, and the average empty tower density in the pulverized coal sedimentation device (34.34 kg/m/s). Wherein the pyrolysis fluidization gas B adopts inert atmosphere, and the gasifying agent D adopts water vapor. By the scheme, the conversion rate of carbon at the gasification outlet in the reactor is 98%, the methane content in the synthesis gas is improved to 19.8%, and the tar yield is 8.5%. The detailed results are shown in Table 1.
[ Example 8]
The reaction scheme was the same as in example 1. The raw materials in the reaction flow adopt lignite+5% K 2CO3. The pyrolysis pressure of the fluidized bed pyrolysis furnace (2) is 0, the pyrolysis temperature is 600 ℃, the average density of pulverized coal in a dense-phase zone (3) of a reactor of the fluidized bed pyrolysis furnace (2) is 550 kg/m 3, and the line speed of a hollow tower in the dense-phase zone (3) of the reactor of the fluidized bed pyrolysis furnace (2) is 0.1 m/s; the gasification pressure of the fluidized bed gasification furnace (8) is 6.5MPa, the gasification temperature is 900 ℃, the average density of pulverized coal is 450 kg/m 3, the average empty tower linear speed in the fluidized bed gasification furnace (8) is 0.2 m/s, the gasification pressure of the rapid bed gasification zone (10) is 6.5MPa, the gasification temperature is 900 ℃, the gasification pressure of the rapid bed steam conversion zone (11) is 6.5MPa, the gasification temperature is 850 ℃, the gasification pressure of the rapid bed methanation zone (12) is 6.5MPa, the gasification temperature is 800 ℃, the average density of pulverized coal in the rapid bed gasification furnace (9) is 150 kg/m 3, the average empty tower linear speed is 1.0 m/s, the combustion pressure of the fluidized bed combustion chamber (7) is 6.5MPa, the combustion temperature is 1100 ℃, the average density is 500 kg/m 3, the average empty tower linear speed in the fluidized bed combustion chamber (7) is 0.2 m/s, the pressure of the fine powder sedimentation/stripper (9) is 6.5MPa, the temperature is 850 m/s, and the average empty tower density in the pulverized coal sedimentation device (34.34 kg/m/s). Wherein the pyrolysis fluidization gas B adopts hydrogen and the gasifying agent D adopts water vapor. By the scheme, the conversion rate of carbon at the gasification outlet in the reactor is 98%, the methane content in the synthesis gas is improved to 20.2%, and the tar yield is 8.0%. The detailed results are shown in Table 1.
[ Example 9]
The reaction scheme was the same as in example 1. The raw materials in the reaction flow adopt lignite+5% K 2CO3. The pyrolysis pressure of the fluidized bed pyrolysis furnace (2) is 0, the pyrolysis temperature is 600 ℃, the average density of pulverized coal in a dense-phase zone (3) of a reactor of the fluidized bed pyrolysis furnace (2) is 550 kg/m 3, and the line speed of a hollow tower in the dense-phase zone (3) of the reactor of the fluidized bed pyrolysis furnace (2) is 0.1 m/s; the gasification pressure of the fluidized bed gasification furnace (8) is 6.5MPa, the gasification temperature is 900 ℃, the average density of pulverized coal is 450 kg/m 3, the average empty tower linear speed in the fluidized bed gasification furnace (8) is 0.2 m/s, the gasification pressure of the rapid bed gasification zone (10) is 6.5MPa, the gasification temperature is 900 ℃, the gasification pressure of the rapid bed steam conversion zone (11) is 6.5MPa, the gasification temperature is 850 ℃, the gasification pressure of the rapid bed methanation zone (12) is 6.5MPa, the gasification temperature is 800 ℃, the average density of pulverized coal in the rapid bed gasification furnace (9) is 150 kg/m 3, the average empty tower linear speed is 1.0 m/s, the combustion pressure of the fluidized bed combustion chamber (7) is 6.5MPa, the combustion temperature is 1100 ℃, the average density is 500 kg/m 3, the average empty tower linear speed in the fluidized bed combustion chamber (7) is 0.2 m/s, the pressure of the fine powder sedimentation/stripper (9) is 6.5MPa, the temperature is 850 m/s, and the average empty tower density in the pulverized coal sedimentation device (34.34 kg/m/s). Wherein the pyrolysis fluidization gas B adopts inert atmosphere, and the gasifying agent D adopts CO 2. Through the scheme, the conversion rate of the gasification outlet carbon in the reactor is 98%, the methane content in the synthesis gas is improved to 19.6%, and the yield of tar is increased by 8.5%. The detailed results are shown in Table 1.
[ Comparative example 1]
The reaction scheme was the same as in example 1. The raw materials in the reaction flow adopt lignite+5% K 2CO3. The pyrolysis pressure of the fluidized bed pyrolysis furnace (2) is 0, the pyrolysis temperature is 600 ℃, the average density of pulverized coal in a dense-phase zone (3) of a reactor of the fluidized bed pyrolysis furnace (2) is 550 kg/m 3, the linear velocity of an empty tower in the dense-phase zone (3) of the reactor of the fluidized bed pyrolysis furnace (2) is 0.1 m/s, the gasification pressure of a fluidized bed gasification furnace (8) is 6.5MPa, the gasification temperature is 900 ℃, the average linear velocity of the pulverized coal is 450 kg/m 3, the average linear velocity of the empty tower in the fluidized bed gasification furnace (8) is 0.2 m/s, the gasification pressure of a fast bed gasification zone (10) is 6.5MPa, the gasification temperature is 900 ℃, the gasification pressure of a fast bed steam conversion zone (11) is 6.5MPa, the gasification temperature is 850 ℃, the gasification pressure of a fast bed methanation zone (12) is 6.5MPa, the gasification temperature is 800 ℃, the average density of the fluidized bed gasification furnace (9) is 150 kg/m 3, the linear velocity of the average tower is 1.0 m/s, the combustion pressure of a fluidized bed combustion chamber (7.5 MPa, the average combustion pressure of the fluidized bed combustion chamber is 3 m/s, and the average density of the fluidized bed combustion chamber is not 3 m/s is 3, and the fine powder is not 3 m/is 3, and the fluidized bed combustion is 3, and the fine powder is not 3 m/is 3, and the combustion and the average density of the fine powder is 3 m/is 3. The pyrolysis fluidization gas B adopts inert atmosphere, and the gasifying agent D adopts water vapor. By the scheme, the conversion rate of carbon at the gasification outlet in the reactor is 90%, the methane content in the synthesis gas is improved to 17.5%, and the tar yield is 7.8%. The detailed results are shown in Table 1.
[ Comparative example 2]
The method adopts a new group PDU gasification reaction device in the prior art (see Bi Jicheng, development and development of a catalytic gasification (one-step method) coal-based natural gas technology [ C ]. A fourth coal-based synthetic natural gas technology economic seminar, 2013 and Urufimbrian) as a raw material, adopts lignite, and adds 10% of potassium carbonate as a catalyst, wherein the linear speed is less than 10m/s, the operating temperature is 800 ℃, the methane content in an outlet gas component obtained by gasification is 14%, but the carbon conversion rate is 90%, no tar product is generated, and the result is shown in Table 1 in detail.
[ Comparative example 3]
The results of the conventional lurgi furnace pressurized fixed bed gasification device (see Wang Peng, et al, development and application of lurgi gasification technology [ J ]. Clean coal technology, 2009,15 (5): 48-51) in the prior art, raw lignite, gasification temperature 850 ℃, methane content in the outlet gas component 8.3%, tar yield 9%, carbon conversion only 90%, are shown in table 1 in detail.
TABLE 1
Any numerical value recited in this disclosure includes all values incremented by one unit from the lowest value to the highest value if there is only a two unit interval between any lowest value and any highest value. For example, if the amount of one component, or the value of a process variable such as temperature, pressure, time, etc., is stated to be 50-90, it means that values of 51-89, 52-88, and 69-71, and 70-71 are specifically recited in this specification. For non-integer values, 0.1, 0.01, 0.001 or 0.0001 units may be considered as appropriate. This is only a few examples of the specific designations. In a similar manner, all possible combinations of values between the lowest value and the highest value enumerated are to be considered to be disclosed.
It should be noted that the above-described embodiments are only for explaining the present invention and do not constitute any limitation of the present invention. The invention has been described with reference to exemplary embodiments, but it is understood that the words which have been used are words of description and illustration, rather than words of limitation. Modifications may be made to the invention as defined in the appended claims, and the invention may be modified without departing from the scope and spirit of the invention. Although the invention is described herein with reference to particular means, materials and embodiments, the invention is not intended to be limited to the particulars disclosed herein, as the invention extends to all other means and applications which perform the same function.

Claims (18)

1. A pulverized coal circulating fluidized bed catalytic gasification methane-increasing device, comprising:
A feeder;
the fluidized bed pyrolysis furnace is connected with the feeder through a feeding inclined pipe;
The fluidized bed gasification furnace is connected with the fluidized bed pyrolysis furnace through a pyrolysis inclined tube;
the lower inlet of the fast bed gasifier is connected with the upper outlet of the fluidized bed gasifier;
the upper inlet of the fluidized bed combustion chamber is connected with the lower outlet of the fluidized bed gasifier;
a fines settler/stripper connected to the fluidized bed pyrolysis furnace through a gasification chute;
The rapid bed gasification furnace comprises a rapid bed gasification zone, a rapid bed steam conversion zone and a rapid bed methanation zone from bottom to top, wherein a steam inlet is arranged on the side wall of the rapid bed steam conversion zone;
The fluidized bed pyrolysis furnace comprises a dense-phase region and an olefin-phase region, wherein the lower part of the side wall of the dense-phase region is respectively provided with a pulverized coal inlet and a gasified semicoke inlet, the pulverized coal inlet is connected with a feeder through a feeding inclined tube, the gasified semicoke inlet is connected with a fine powder sedimentation/stripping device through a gasification inclined tube, the side wall of the dense-phase region is provided with a pyrolysis semicoke outlet which is connected with the fluidized bed gasification furnace through a pyrolysis inclined tube, and a cyclone separator of the fluidized bed pyrolysis furnace is arranged in the olefin-phase region;
the lower part of the side wall of the fluidized bed gasification furnace is provided with a pyrolysis semicoke inlet which is connected with the fluidized bed pyrolysis furnace through a pyrolysis inclined tube;
The fine powder sedimentation/stripping device comprises a stripping section, a fine powder sedimentation section and a fine powder sedimentation/stripping device cyclone separator, wherein a stripping gas inlet is arranged at the lower part of the side wall of the fine powder sedimentation/stripping device and is used for receiving stripping gas, a semicoke outlet is arranged at the lower part of the side wall of the fine powder sedimentation/stripping device and is connected with a fluidized bed pyrolysis furnace through a gasification inclined tube, and a synthesis gas outlet is arranged at the top of the fine powder sedimentation/stripping device and is connected with a gas outlet of the fine powder sedimentation/stripping device cyclone separator and is used for discharging synthesis gas.
2. The apparatus according to claim 1, wherein a pyrolysis fluidization gas inlet is provided at the bottom of the fluidized bed pyrolysis furnace for receiving pyrolysis fluidization gas, and/or a pyrolysis gas outlet is provided at the top of the fluidized bed pyrolysis furnace, which is connected to a gas outlet of a cyclone separator of the fluidized bed pyrolysis furnace for discharging pyrolysis gas.
3. An apparatus according to claim 1 or 2, characterized in that the bottom of the fluidized bed combustion chamber is provided with an ash discharge port, which is connected to an ash tank.
4. The apparatus according to claim 3, characterized in that a synthesis gas return is provided in the side wall of the rapid bed methanation region;
And/or a gasifying agent inlet is arranged at the lower part of the side wall of the fluidized bed gasifier, and the gasifying agent inlet is used for receiving gasifying agent.
5. The apparatus according to claim 1 or 2, wherein a rapid bed cyclone is provided inside the fines sedimentation/stripping vessel, which is connected to an upper outlet of the rapid bed gasifier.
6. The apparatus of claim 1 or 2, further comprising an aftertreatment system comprising:
a first gas-solid fast separator connected to a pyrolysis gas outlet of the fluidized bed pyrolysis furnace;
The gas-liquid separation device is connected with the first gas-solid rapid separator;
A second gas-solids fast separator connected to the synthesis gas outlet of the fines settling/stripper;
and the gas separation device is connected with the second gas-solid rapid separator and the gas-liquid separation device.
7. The apparatus of claim 1 or 2, further comprising a catalyst system comprising a catalyst recovery device and a catalyst loading device, wherein the upstream of the catalyst recovery device is connected to the ash pot and the downstream is connected to the catalyst loading device, and wherein the upstream of the catalyst loading device is connected to the catalyst recovery device and the downstream is connected to the feeder.
8. A method for increasing methane yield by catalytic gasification of pulverized coal circulating fluidized bed, which adopts the device as claimed in any one of claims 1 to 7, and comprises the following steps:
(a) The pulverized coal raw material is sent into a fluidized bed pyrolysis furnace by a feeder, and is mixed with high-temperature gasified semicoke in the fluidized bed pyrolysis furnace to be heated, and the pulverized coal undergoes pyrolysis reaction to generate pyrolysis semicoke and pyrolysis gas;
(b) The pyrolysis semicoke enters a fluidized bed gasifier through a pyrolysis inclined tube, contacts with gasifying agent, and is subjected to gasification reaction in the fluidized bed gasifier and the rapid bed gasifier to generate synthesis gas and carbon-containing gasification semicoke;
(c) The synthesis gas enters a fine powder sedimentation/stripping device to separate high-temperature gasification semicoke, and the high-temperature gasification semicoke enters a fluidized bed pyrolysis furnace through a gasification inclined tube;
(d) The carbon-containing gasified semicoke downwards enters a fluidized bed combustion chamber from a fluidized bed gasifier to undergo a combustion reaction to produce ash slag and high-temperature gas, and the high-temperature gas upwards enters the fluidized bed gasifier to be used as a gasifying agent.
9. The method of claim 8, wherein the pulverized coal feedstock comprises pulverized coal and at least one of a catalyst and biomass.
10. The method of claim 9, wherein the catalyst comprises at least one of an alkali metal, an alkaline earth metal, and a transition metal.
11. The method according to any one of claims 8 to 10, wherein the pulverized coal raw material is fed into a dense phase zone of the fluidized bed pyrolysis furnace by a feeder, mixed with high-temperature gasified semicoke in the dense phase zone and heated, the pulverized coal undergoes pyrolysis reaction to generate pyrolytic semicoke and pyrolysis gas, the pyrolytic semicoke enters the fluidized bed gasification furnace through a pyrolysis inclined tube, the pyrolysis gas entrains fine pulverized coal, enters an olefin phase zone upwards to carry out gas-solid separation through a cyclone separator of the fluidized bed pyrolysis furnace, solids return to the dense phase zone, and gas leaves the fluidized bed pyrolysis furnace to sequentially enter a first gas-solid rapid separator and a gas-liquid separation device to remove fly ash and tar, and then enters the gas separation device.
12. The method according to any one of claims 8 to 10, wherein the fluidized bed pyrolysis furnace has a pyrolysis pressure of 0 to 6.5MPa and a pyrolysis temperature of 400 to 800 ℃, and/or the fluidized bed pyrolysis furnace has an average density of pulverized coal of 200 to 550kg/m 3 and a superficial linear velocity of 0.1 to 1.0m/s.
13. The method of any of claims 8-10, wherein the pyrolysis semicoke enters a fluidized bed gasifier, contacts a gasifying agent, undergoes gasification reactions in the fluidized bed gasifier and a fast bed gasifier to produce synthesis gas and carbonaceous gasification semicoke, and the fast bed gasifier undergoes gasification reactions while circulating synthesis gas is fed into a fast bed methanation region to undergo methanation reactions.
14. The method according to any one of claims 8 to 10, wherein the fluidized bed gasifier has a gasification pressure of 0 to 6.5MPa, a gasification temperature of 700 to 1200 ℃, an average pulverized coal density of 200 to 450 kg/m 3, an average superficial linear velocity of 0.2 to 1.2 m/s, and/or the rapid bed steam shift zone has a gasification pressure of 0 to 6.5MPa, a gasification temperature of 700 to 1000 ℃, and/or the rapid bed methanation zone has a gasification pressure of 0 to 6.5MPa, a gasification temperature of 700 to 900 ℃, and/or the rapid bed gasifier has an average pulverized coal density of 50 to 150 kg/m 3, an average superficial linear velocity of 1.0 to 3.0m/s.
15. The process according to any one of claims 8-10, wherein the synthesis gas exiting the rapid bed gasifier is entrained with unvaporized semi-coke fines, the gas-solid separation is performed by first entering a rapid bed cyclone, solids fall into the stripping section of the fines settler/stripper, the gas enters the settling section of the fines settler/stripper, and/or the gas exiting the rapid bed cyclone enters the settling section of the fines settler/stripper and the fines settler/stripper cyclone, solids are further separated, solids fall into the stripping section of the fines settler/stripper, the gas exits the fines settler/stripper into a second gas-solid rapid separator, fly ash is removed, and then enters the gas separation device, and the gas fraction exiting the gas separation device is recycled back to the rapid bed methanation zone.
16. The method according to any one of claims 8 to 10, wherein a stripping gas is introduced into the stripping section of the fines settler/stripper, and the solids of the stripping section are stripped to obtain a high temperature gasified semicoke, which enters the fluidized bed pyrolysis furnace via a gasification chute.
17. The method according to any one of claims 8 to 10, wherein the carbonaceous gasification semicoke enters the fluidized bed combustion chamber downwards from the fluidized bed gasification furnace, contacts with an oxidant to generate combustion reaction, ash and high-temperature gas are produced, the high-temperature gas enters the fluidized bed gasification furnace upwards as the gasifying agent, and the ash is discharged.
18. The method according to any one of claims 8 to 10, wherein the fine powder settling/stripping vessel has a pressure of 0 to 6.5MPa, a temperature of 700 to 1200 ℃, an average density of pulverized coal of 350 to 550 kg/m 3, an average superficial linear velocity of 0.1to 0.5m/s, and/or the fluidized bed combustor has a combustion pressure of 0 to 6.5MPa, a combustion temperature of 800 to 1500 ℃, an average density of 300 to 450 kg/m 3, and an average superficial linear velocity of 0.2 to 0.6 m/s.
CN201910905954.XA 2019-09-24 2019-09-24 Catalytic gasification device and method for pulverized coal circulating fluidized bed Active CN112625756B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201910905954.XA CN112625756B (en) 2019-09-24 2019-09-24 Catalytic gasification device and method for pulverized coal circulating fluidized bed

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201910905954.XA CN112625756B (en) 2019-09-24 2019-09-24 Catalytic gasification device and method for pulverized coal circulating fluidized bed

Publications (2)

Publication Number Publication Date
CN112625756A CN112625756A (en) 2021-04-09
CN112625756B true CN112625756B (en) 2025-07-25

Family

ID=75283364

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201910905954.XA Active CN112625756B (en) 2019-09-24 2019-09-24 Catalytic gasification device and method for pulverized coal circulating fluidized bed

Country Status (1)

Country Link
CN (1) CN112625756B (en)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114774169B (en) * 2022-04-26 2024-08-20 中国科学院工程热物理研究所 Gasification device, gasification method, and thermochemical reaction device

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108893130A (en) * 2018-08-17 2018-11-27 中石化（洛阳）科技有限公司 A kind of fine coal destructive distillation device and fine coal method for destructive distillation
CN109401788A (en) * 2017-08-17 2019-03-01 中国石油化工股份有限公司 The combined fluidized bed reaction unit and reaction method of catalytic gasification coupling pyrolysis
CN109652147A (en) * 2017-10-12 2019-04-19 中国石油化工股份有限公司 Recirculating fluidized bed pyrolysis-gasification installation and method
CN211199135U (en) * 2019-09-24 2020-08-07 中国石油化工股份有限公司 Catalytic gasification yield-increasing methane device of pulverized coal circulating fluidized bed

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2413749C2 (en) * 2009-04-21 2011-03-10 Открытое акционерное общество "Украинский институт по проектированию нефтеперерабатывающих и нефтехимических предприятий" (ОАО "УКРНЕФТЕХИМПРОЕКТ") Procedure for complex coal processing and installation for its implementation
CN102465043B (en) * 2010-11-01 2013-07-31 中国科学院过程工程研究所 Multi-section fractional pyrolysis gasification device and method for solid fuel
CN102585947B (en) * 2011-12-14 2016-05-04 新奥科技发展有限公司 A kind of method and apparatus that is contained the gas of methane by coal preparation
CN103980948A (en) * 2014-06-11 2014-08-13 华东理工大学 Coal powder pyrolysis and gasification method
CN106833753A (en) * 2017-01-17 2017-06-13 王树宽 A kind of up flow type pyrolysis and downstriker gasification coupling prepare the device and method of coal tar oil and gas

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109401788A (en) * 2017-08-17 2019-03-01 中国石油化工股份有限公司 The combined fluidized bed reaction unit and reaction method of catalytic gasification coupling pyrolysis
CN109652147A (en) * 2017-10-12 2019-04-19 中国石油化工股份有限公司 Recirculating fluidized bed pyrolysis-gasification installation and method
CN108893130A (en) * 2018-08-17 2018-11-27 中石化（洛阳）科技有限公司 A kind of fine coal destructive distillation device and fine coal method for destructive distillation
CN211199135U (en) * 2019-09-24 2020-08-07 中国石油化工股份有限公司 Catalytic gasification yield-increasing methane device of pulverized coal circulating fluidized bed

Also Published As

Publication number Publication date
CN112625756A (en) 2021-04-09

Similar Documents

Publication Publication Date Title
EP3566770B1 (en) A process for catalytic gasification of carbonaceous feedstock
CN107760377B (en) Fluidized bed and fixed bed combined coal catalytic gasification reaction device and method thereof
CN106590761B (en) Fluidized bed reaction device and reaction method for preparing methane-rich synthesis gas through catalytic coal gasification
CN108946661B (en) Method and system for preparing hydrogen through biomass gasification
WO2010124066A2 (en) Integrated, high-efficiency processes for biomass conversion to synthesis gas
CN109652147B (en) Circulating fluidized bed pyrolysis-gasification device and method
CN102021037A (en) Method and apparatus for preparing methane by catalytic gasification of coal
CN102277200A (en) Method for preparing coal gas by virtue of pulverized coal grading gasification
CN107760384B (en) Efficient device and method for preparing methane-rich synthesis gas through catalytic coal gasification
CN100441663C (en) Fluidization hydrogenation liquefaction method for coal
CN102234545B (en) A method for producing synthesis gas by gasification of carbonaceous materials
CN109401788A (en) The combined fluidized bed reaction unit and reaction method of catalytic gasification coupling pyrolysis
CN105087078A (en) Indirect pyrolysis system and pyrolysis method thereof
CN109401794A (en) The combined fluidized bed reaction unit of staged conversion and reaction method
CN112625756B (en) Catalytic gasification device and method for pulverized coal circulating fluidized bed
CN211199137U (en) Circulating fluidized bed pulverized coal pyrolysis-gasification device
CN211199135U (en) Catalytic gasification yield-increasing methane device of pulverized coal circulating fluidized bed
CN211199136U (en) Device for fluidized catalytic gasification of pulverized coal
KR20140080453A (en) Circulating Fluidized Bed Gasifier Equipped with Heat Exchanger Therein
CN112625757B (en) Device and method for fluidized catalytic gasification of pulverized coal
CN107916140B (en) Circulating fluidized bed-entrained flow combined gasification method and device
CN111621340B (en) High-efficiency catalytic gasification system and method for coal
CN116731752A (en) Device and method for hydrogen capture of carbon dioxide from coal/biomass chemical chain
CN112625755B (en) Circulating fluidized bed pulverized coal pyrolysis-gasification device and pulverized coal pyrolysis-gasification method
CN109401793B (en) Pulverized coal gasification downer reaction device and reaction method

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant